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(9.0767 kg/s), and 75624.1 lbm/hr (9.5286 kg/s), respectively. Likewise the minimum mass flows are (in the same order): 358.63 lbm/hr (0.0452 kg/s), 7203.77 (0.9077 kg/s), and 7562.41 (0.9529 kg/s). The mass fraction of the strong, weak, and vapor streams are xS = 0.3988, xW = 0.3689, and xV = 1.0 (assumed). A decrease in mass flow through the system manifests itself in the reduction of work and heat interactions of the cycle for a given output as seen in Figures 5.2 and 5.3. Minimum pump work, boiler heat input and absorber heat rejection are: 0.724 Hp (0.540 kW), 331,566 Btu/hr (97.18 kW), and 321,117 Btu/hr (94.11 kW). The ideal cooling capacity under these conditions is 9130.26 Btu/hr (2.68 kW). Figure 5.4 concludes that at least 60% efficient expansion is required to obtain any cooling capacity. Below this point, the exhaust temperature of the expander exceeds the assumed temperature of the substance to be cooled (85 °F). This effect is also evidenced in the plot of the expander isentropic efficiency versus the cycle thermal efficiency (Figure 5.5). Figure 5.2 Pump work variation with expander efficiency Figure 5.3 Boiler heat input and absorber heat rejection vs. expander efficiency Figure 5.4 Cycle cooling capacity as a function of expander efficiency Figure 5.5 Cycle thermal efficiency vs expander efficiency Thermal efficiency increases linearly with expander efficiency; however, a sudden increase in slope occurs at approximately ηe = 0.6 at which point the cooling effect begins to enhance the thermal efficiency of the cycle. The highest achievable thermal efficiency for the given operating conditions is 7.22%. The mass fraction of ammonia entering the expander was analyzed more closely to judge the assumption of pure vapor leaving the rectifier and to determine the impact that trace quantities of water have on the cycle performance. The analysis was carried out for an ideal expander. Figure 5.6 shows the profound negative effect on cooling capacity. The cooling capacity diminishes to zero rapidly as trace amounts of water are introduced into the expander stream up to only 2.5% by mass. Boiler heat input is reduced from 331,566 Btu/hr (97.18 kW) to 320,934 Btu/hr (94.06kW); however, thermal efficiency is reduced 9.26% from 7.22% to 6.55% because of the lost cooling benefit. Another concern is that the expander exhaust temperature drops below the mixture dew point as shown in Figure 5.7. At a 2.5% water vapor concentration by mass, the mixture quality is 0.967. This most likely is not an issuePDF Image | Optimization of a Scroll Expander Applied to an Ammonia/Water Combined Cycle System for Hydrogen Production - Paper No. 1645
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